Alkylation method



Nov. 30, 1948. V A, R, GovLDsBY ET Al. 2,454,869.`

ALKYLATION METHOD AR. GoLDsBY ET AL ALKYLATION METHOD Filed'Feb. 24, 1943 2 Sheets-Sheet 2 EAcToR OLEFINS ISOBUTANE o sE'r'rER ARTHUR RGOLDSBY CLAUDE W WATSON lN ENTORS lsoBuTANE l oLEFlNs ACFD ISO BUTANE Patented Nov. 30, 1948 ALKYLATION METHOD Arthur R. Goldsby, Beacon, and Claude W. Watson, Tuckahoe, N. Y., assignors to The Texas Company, New York, N. Y., a corporationof Delaware Application February 24, 1943, Serial No. 476,896'

3 Claims. l

This invention relates to the catalytic alkylation of a hydrocarbon or other organic compound having a replaceablehydrogen atom with a suitable alkylating agent, such as an olen, for the production of gasoline hydrocarbons of high antiknock value suitable for aviation gasoline and motor fuel, or for the production of valuable alkylated organic compounds for other purposes.

One of the principal objects of the invention is to provide an improved method of alkylating such an organic compound having a replaceable hydrogen at-om with 'an alkylating agent to avoid local accumulation of alkylating agent, such as an olen, in any portion of the reaction zone to thereby avoid objectionable side reactions of the alkylating agent in the presence of 'the catalyst, whereby high yields of a superior quality of alkylate are obtained while effecting economy in installation and operating expense.

A further object of the invention is to provide a novel catalytic alkylation method of this character to obtain improved quality and yield of alkylate and increased catalyst life for a given set of operating conditions, -or to obtain increased capacity without sacrifice of quality and yield of alkylate or reduction in catalyst life, from a given unit under different and more economical operating conditi-ons.

Another object of the invention is to provide an improved method of alkylating an isoparafln with a suitable alkylating agent, such as an olenn, wherein the alkylating agent is introduced into a mechanically-agitated body or stream of the hydrocarbons and catalyst at a large number of spaced points, and in fine subdivision or small droplets from each of the points, whereby the alkylating agent is promptly reacted without polymerization or other objectionable side reactions, and good catalyst life and high quality alkylate are secured without the necessity of maintaining the very high isoparaflin concentration in the reacted mix previously thought necessary to attain these results.

Still another object of the invention is to provide novel apparatus for carrying out the above methods.

Other objects and advantages of vthe invention will be apparent from the following description when taken in conjunction with the accompanying drawing and appended claims.

Various catalytic alkylation processes for alkylating an isoparaffin with an olefin or yother sultable alkylating agent for the production of gasoline hydrocarbons of high anti-knock value are known. These involve 'the use of catalysts such (Cl. Zilli-683.4)

-as strong sulfuric acid, hydrofiuoric acid, aluminum chloride, BFS-water complex, etc. The best known process which is now widely used ona commercial scale is the sulfuric acid alkylation process. Various reactors, such as the pump and time tank reactor, jet type reactor. andpropeller type of mixer such as the Stratco reactor, have been used in this process. In these various processes, it is an objective to preferentially react the olefin with the isoparalin to produce the desired alkylate and minimize side reactions of the olen with itself or with Vthe catalyst, which side reactions cause deterioration in quality and yield of the product and reduce catalyst life.

In order to accomplish this objective, it is customary to use a feed inwhich the isoparaflin is in substantial molar excess of the olefin, and also to recycle hydrocarbon products or an emulsion vof catalyst with hydrocarbon products in order to build up a very high ratio of isoparaiiin to olefin at the point of contact of the olefin with the alkylation catalyst. Moreover, it is approved practice to `carefully fractionate and precondition the feed to remove normal paraln diluents and impurities, and to maintain a very high isoparafn concentration in the hydrocarbon phase of the reacted mix, such as an isobutane concentration of -70% or more by volume in the hydrocarbon phase undergoing reaction, where alkylate of the highest Iclear octane is desired.

.It has also been customary to employ two or more reactor systems in series, with the olen feed split between the plurality of reactors. In all the systems heretofore suggested or employed, the olefin feed has been introduced at one point -or localized area, or at two or three points at most of any reactor system. While very good operation has been secured in the past with the expedients mentioned above, including high isoparanin-to--olefin feed ratio, high emulsion recycle ratio, split olen feed, and high isoparafn concentration in the hydrocarbon phase of the reacted mix, there are still some side reactions which show up largely in reduction in yield and quality of thealkylate and in catalyst deterioration, thereby reducing the life of the catalyst and kincreasing the cost of the process per unit volume of alkylate and finished octane gasoline produced. Further, the necessity for maintaining the very high isobutane concentration in the reacted mix represents one of the most expensive items -of the process, due to the expense involved in the instaliationand operation of the fractionating euuipment required for separating isobupipe or pipes.

ously proposed to inject the olefin into the reactor f in finely-divided form through an aluminum or other porous member having openings of substantially capillary size, these openings have been concentrated in one local area of the reactor. Consequently, even though the olefin was introduced in small streams, the various streams were concentrated in a small portion of the volume of the reaction mass. Moreover, in this type of reactor, there was no mechanically-maintained agitation and circulation as herein defined, since the force of injection through the jet was relied on to churn up the contents of the reactor and produce a turbulent mixing action without directional flow characteristics. The presentinvention is distinguished by the use of mechanicallymaintained agitation and circulation independent of the olefin feed orices or openings, and by the spacing of the small olen feed openings throughout a substantial extent of the reaction zone so that local accumulation of olen is avoided. By the expression mechanically-maintained agitation as used herein throughout the description and claims, it will be understood some form of power-driven agitator, pump, turbine or propeller for imparting vigorous agitation and circulation to the contents of the reactor independently of the olen feed is intended.

duced into this recirculating stream at one or at most two or three points from a relatively large mixer such as the Stratco reactor, wherein the olefin feed is introduced into the internal recirculating stream at a single point. In an eiort to overcome the objectionable side reactions in such equipment, it is customary to circulate the emulsion stream at high velocity past the point of introduction of the olen stream. However, this `does not wholly accomplish the desired objective, apparently due to the fact that the olen is introduced in a relatively large stream from the large pipe opening, thereby resulting in local accumulation.

The present invention is distinguished from this practice by the use of a very large number of small openings spaced throughout a substantial portion of the length of the recirculating stream, whereby such local accumulation cannot occur. For example, the openings may each be less than one-quarter inch in diameter and smaller down to capillary size;` and there may be as many as from fifty up to several thousand or more openings for the same overall olefin feed rate distributed with fairly equal spacing throughout one-quarter to one-half or more of the length of the recirculating passage in the reaction zone. Moreover, the spacing of the variious points of introduction is correlated with the velocity of flow and volume vof the recirculating stream, whereby olefin introduced into an increment of the recirculating stream at one point The same is true of the propeller per unit of time is substantially completely reacted by the time said increment receives the next portion of olen feed. This does not imply that the olefin has reacted by the time said increment moves forward to the next opening in series, since the openings are also spaced laterally or circumferentially of the circulating stream s0 that different increments of the circulating stream receive oleiin from adjacently-positioned openings in the direction of ow. By the eX- pression reacted as used immediately above, it is to be understood that this does not necessarily mean that the alkylation reaction with the isoparamn of that olen has been completed but it does imply that the olen or other alkylating agent has been removed as a factor causing local overheating and objectionable side reactions lwhich impair the quality of the product as determined by the percentage boiling above the theoretically-predicted product, such as octanes for 'isobutane-butylene alkylation, heptanes for isobutane-propylene alkylation, etc., and which cause catalyst deterioration as determined by catalyst life.

The present invention eiectively inhibits and limits the localized concentration and buildingup of alkyl sulfate in the sulfuric acid catalyst. Where the oleiin is introduced in very small size, such as from openings approaching capillary size, some overlapping of olefin from adjacent openings is permissible, since the olein will not accumulate to any greater extent than the initial accumulation resulting from introduction from a larger size orice of about one-eighth to one-quarter inch diameter. Apparently, the first fraction of a second of contact of the oleiin with the acid is the critical time. When the olefin is properly introduced, and the concentration of the olefin or its reaction product with the acid is maintained at a very low iigure, the olen may remain in the acid with safety and without adverse results for relatively long periods.

The overall or average concentration of the oleiin or alkyl sulfate in the acid and which can be f measured will, of course, always be much less than the concentration immediately at the point of olen entry. But when operating by the process of this invention, the concentration at the immediate point of entry is very greatly reduced: and this reduction may be considerably greater than the reduction in the overall or average concentration Which can be measured. In other words, this invention departs from prior practice in this art in that it is primarily concerned with greatly reducing the concentration of olen at the immediate point of entry and in any portion of the reacting mix for the rst fraction of a second to a few seconds followingr the introduction of the olen. In considering the concentration of olefin in the acid, this invention is concerned with very small units of the acid immediately surrounding or contacting the introduced olefin droplets and not necessarily in the overall reaction mixture which is susceptible to an average measurent of alkyl sulfate concentration. By combining the feature of finely lsubdividing the olefin with the finite spacing of the different and large number of points of 01ei'in introduction so as to prevent any substantial accumulation or build-up of olen in any increment of the acid in the reaction mixture, local overheating which is apparently conducive to obiectionable side reactions is effectively avoided. This avoidance of the build-up and accumulation of alkyl ester concentration in the acid to- .5 @other with the avoidance of localized overheating and .side reactions such as polymerization and hydropolymerization are apparently responsible for the vini-proved catalyst life and other advantages attained 'by the process of the present invention.

1t will be understood lthat the statements in the preceding paragraph apply to alkylating conditions including a high isoparailin-to-olen ratio :and Va proper proportion lof A:is'ololuta'ne in the hydrocarbon `,phase of the reacted mix. Moreover, in .accordance `with the presen-t invention, not :only is .the .olefin distributed throughout the reacting 'by multitudinous point injection, but

also the feed isoparaiiin, :such as isobutane, or a substantial portion thereof may likewise be disseminated widely and more uniformly throughout the reacting mix and thus :more homo.- geneously emulsied with and/or dissolved in the acid. This is accomplished by mixing all ro1- a .portion of the isobutane fresh feed 'and the external isobutane recycle with the olefin `feed, and introducing the mixture into the reaction zone through the very large number `oi openings .spaced widely throughout the said zone.

It has `been postulated that the alkylation reaction takes place vbetween is'obutane dissolved in the acid and olefin at the acid hydrocarbon interface; yand it is believed that the fail-ure of prior alkylation equipment in preventing objectionable sid-e reactions has been largely due to practical mechanical limitations on `the emciency of agitation and mixing or the velocity 'of emulsion recycle in :getting isobutane dissolved uniformly throughout the acid .and maintaining th'e required equilibrium between the isobutane in the acid phase and isobutane in the hydrocarbon phase. The present invention `overcomes these mechanical .difficulties bjy initially distributing .the

yisobutane in inely-divided form throughout the acid 4in the reaction zone, rather than by vadding the isobutane in one or a few large streams and then attempting to get uniform distribution solely by -etlicient mechanical mixing orhigh-speed recirculation Witlo turbulent ilo-W. The proper distribution of dissolved iscbutane throughout the acid phase, and the proper equilibrium between the isobutane in the acid phase and the isobutane in the hydrocarbon phase is thereby .accomplished in a practical and economicalmanner, with the further advantage that the power-requirements for the mechanical agitation or the recirculation may be substantially reduced while still obtaining improved results.

Further, the ratio of isobutane to olen at the point of olen entry and contact with the acid, termed the contact ratio, is at `the same time increased far beyond anything heretofore secured or deemed practical Thus, another object ofthe present invention in obtaining a very'high effective contact ratio 4at the immediate points of ole- -n entry is accomplished at .a much lower `cos-t than for so-called contact ratios of about 590:1-to 1200: 1 heretofore specified, which latter were pre viously considered to be about the highest practically attainable. In the present case, elective contact ratios .of about 1500z1 to 2,000,000:l and higher are readily secured. Since the rst fraction of a second following initial contact ofthe olefin With the acid appears to be the-critical time, and the olen is then fixed or converted to an inactive form so far as objectionable side reactions are concerned, the expression eecti've contact ratio at the immediate point of olefin entry is vused in the description and claims to' 6 .signify the product obtained by .isoparafn-olen `feed ratio times the internal isoparamn recycle (which is the isoparaln or risobutane content of 'the recycled emulsion) 'to hydrocarbon feed ratio times the number `of :olefin -feed openings in the 'reactor system (each opening being of sunlcientlysma'll 'size and the various openings spaced suciently far apart that each oleiin droplet issuingfrom any opening may be considered as a unit forwall practical purposes). For example, with .a .3f 1 isobutane-olefin feed ratio, a relatively low 10:1 internal isobutane recycle ratio, and 50 olefin' entry 'points of small size distributed throughout 'the .reaction zone in accordance with the 1,present invention, the eifective isobutane to olefin @contact ratio at the immediate point of Aoleiin entry is v'('3 101 50) :1 or 1500:1. Likewise, with :a 5:1 .feed ratio, a 200:1 internal recycle ratio fand .2000 olefin entry points, the effective contact ratio is 2,000,000:1. In this connection, it should be borne in `mind that in previous alkylation units, such as `the propeller mixer type, operating with' high velocities of recirculating emulsion .and which have been described as having `contact ratios'up to about 1200:1, the effective contact ratio :at the immediate point of olefin entry is actually much lower than this, because the 'olen is .introduced in a relatively large stream and is therefore accumulated or concentrated at the immediate locus lof the relatively large pipe .opening where the olefin enters the circulating mix as a stream (as yopposed to dispersed tiny droplets). Therefore, the quantity of olen in this stream iat 'said locus (which represents the irst fraction of asecond of contact with the acid) is as much as sixty-four or more times greater the unitary size or quantity of the olefin droplet mentioned above, giving an eifective contact ratio iat the .immediate point of olelin entry as above deiined of less than 20:1.

By following the principles of the present invention, improved results in the form `of increased yield foi 'better quality alkylate and improved catalyst life can be secured from a given set of opf isobutane concentration in the reacted mix to be substantially lowered, such :as to about ell-60% and preferably around 50%, and still secure yields and'quality of alhylate and catalyst life comparable to those formerly obtained under only optimum conditions with the very high isobutane concentrations, with resultant increase in capacity and greatly improved economy in installation and operating expense.

Furthermore, due tothe more positively-directed reaction of the isopara-iiin with the olefin under ythe conditions set forth herein, the contact .time Vfor thereactlon may be substantially reducedover that now employed, thereby resulting in greater capacity for the same size of unit. Contact time as employed herein means the hydrocarbon volume of the recirculating stream divided by the rate of` fresh hydrocarbon feed,

which latter includes the external isoparamn recycle. In conventional sulfuric acid alkylation,

itis customary to employ a contact time of about :vacunas 20 minutes minimum, and generally about 30 minutes o1' more. In accordance with the present invention, the contact timei may be reduced to about minutes or even less. 'For example, with a high acid-to-hydrocarbonl ratio in excess of about 1:1 by volume, such as about 113:1 to 2:1, and with acceleratedv settling-as by the aid of a centrifuge, the contact time'may bereduced to about 1-5 minutes.` Moreover, power. requirements may be reduced, since the need for extremely high velocities of flow of the recirculated stream is lessened. Thus, in a reactor of the propeller-mixer type normally operating to e'ect a complete turnover of the contents of the reactor once every thirty to forty seconds, for example, the rate of recirculation may be reduced in accordance with the present invention so as. to secure a complete turnover in about' seventy-five toa hundred seconds or more, While still obtaining'improved results. I D f The present invention is applicable to the alkylation of any low-boiling isoparain with'any normally gaseous or normally liquid olen. Thus, the isoparain may be isobutane, isopentane or isohexane. The olefin maybe ethylene, propylene, butylenes, pentylenes, heX-ylenes, other higher boiling monomeric olens or certain selected fractions of cracked naphthas, olefin polymers such as di-isobutylene, tri-isobutylene, cross-polymers of isobutylene and normal butylenes, and various mixed or non-selective polymers. In place of olefms as the alkylating agent, various alkyl esters, such as the sulfates, chlorides, fiuorides, etc., may be used. Moreover,

various aliphatic alcohols and ethers, such as tertiary butyl alcohol, isopropyl alcohol, butyl ether, etc., may be employed as the alkylating agent, particularly with catalysts which have tolerance for water liberated in the reaction. The

expression alkylating agent is used herein throughout the description and claims todenote any of the above compounds which react with an isoparain or other organic compound having a replaceable hydrogen atom in this alkylation reaction to produce alkylated hydrocarbons, In place of the pure hydrocarbons or other alkylating agents, it is of course to be understood that various renery fractions, such as a C4, ca -C4, Cri-C5, Cs, etc. may be employed;y

The present invention is applicable to the use of any of the well-known alkylation catalysts, such as sulfuric acid, hydrofluoricacid, aluminum chloride-hydrocarbon complex, 'BF3.nH2O, chlorsulfonic acid, iuorsulfonic acid andthe like. The various conditions for the reactions employing these catalysts are well known; and conventional conditions coupled with theffeatures of the .present invention as set forth above may be used. By Way of example,V the invention is more particularly described herein inconnection with the use of strong sulfuric acid as the catalyst; but it is to be understood that this is'by way offillustration and not limitation.

The conventional conditions for sulfuric acid alkylation which may be used include an isoparafn-to-olefin feed ratio of about 3:1 to 8:1 or higher. a recycle ratio of emulsion or hydrocarbon to feed hydrocarbons (thelatter including the external isobutane recycle) of about 10:1 to 200:1 or more. an acid concentration in the reaction zaneof about 85 'to 96%, that is, about S23-96% for C4 and about Z55-92% for` Cs, with make-up acid of about 94-l00% strength, a temperature of about -100" F. and preferably about 35-60" F.,

`:and suiiicient'pressure to maintain. the hydrocarbon reactants in the liquid phase. In addition, the conventional acid-to-hydrocarbon ratio of around 1:1 by volume and the conventional contact time of about 20-60 minutes may be used; but, as pointed out above, the present invention enables higher acid-to-hydrocarbon ratios up to `2:1 and much shorter contact times of down to as little as 1-5 minutes to be employed with advantageous results. Likewise, the high isoparaflin concentration of around (iO-70% by volume in the hydrocarbon phase of the reacted mix may `be used, although the present invention enables much lower isoparaiiin concentrations of the order of about Llil-50% to be employed with the greatly improved economies and increased capacity specified above.

The invention is more particularly illustrated in the attached drawing which discloses preferred embodiments thereof, and wherein:

Fig. 1 is a diagrammatic View of one form of reactor of the propeller-mixer type with accompanying accessory equipment;

Fig. '2 is a diagrammatic View of a modified propeller-mixer;

Fig.l 3 is a diagrammatic view of Still another modification of the propeller-mixer type; and

Fig. 4 is an enlarged partial elevational View of the perforated liner II of Fig. 1.

Referring to Fig. 1, a reactor of the propellermixer type is shown having a casing or shell I 0 provided with an interior lining Il forming an annular chamber I2 therebetween. Positioned within the shell is an interior hollow tube I3 which is open-ended and spaced from the wall of the shell. A pump I4 is located adjacent the lower end of tube I3 and is connected by a shaft I 5 to a suitable power source (not shown). Operation of the pump causes internal recirculation of the contents of the reactor upwardly through the channel I 6 within the hollow tube I3 and thence downwardly through' the annular space I1 between tube I3 and liner II, as indicated by the arrows. v

Alkylation catalyst such as sulfuric acid is supplied to the interior recirculating passage of the reactor'by line 20, which extends through the annular chamber I2 and liner Il and opens directly into the space Il.' Isobutane or other suitable isoparalin feed is introduced by line 2l. A portion or all of the isobutane may be passed byline 22 to' the olefin feed line 23 to thereby provide a mixed hydrocarbon feed in which the isobutane is in substantial molar excess of the olen. The hydrocarbon feed is introduced under pressure and in liquid phase into the annular chamber I 2 of the reactor. Liner II is constructed of an acid-resisting porous or perforated material, such as porous alundum or a perforated alloy metal. A large number of olefin charge ports or openings 25 are thus provided surrounding the recirculating passage through Whichthe emulsion is forced by pump i4. The hydrocarbon feed is maintained within the annular chamber I2 at a higher pressure than that maintained within the interior of the reactor proper, whereby the olefin feed passes into the circulating emulsion stream, as indicated in the menaces,

inetal liner having-jperforations of. about 11s. to 1A; inch in. diameter'. with centers spacedv about 1 to 6 inches or more apart in all: directions about the periphery .of the reactor. In a. commercial size reactor, this will provide from. 100 to 2000 or more openings. Where an alundum liner is employed, of course there will bean extremely large number of ports of capillary size. In any event, it is desirable to have-more thanl.0 to 20 openings which are not. only rather evenly distributed around the periphery of the reactor but also extend. throughout a substantial portion of the length. of the recirculating ilow passage.

Where very small openings are. used, it may be desirable to lter the liquefied hydrocarbon feed to remove any finely-divided suspended matter from the` charge. The rate of feed can be controlled by the differential pressure-between the annular chamber l2 and the interior `of the reactor. The liqueed hydrocarbon jetting through the openings in fine droplets under the pressure differential employed coupled with the sweeping action of the recirculating. emulsion past ythe openings minimizes plugging thereof; and finely-divided carbon or other particles normally present or formed in the acid is effectively prevented from lodging in thefopenings. In practice, pressure` pulsations applied to annular chamber l2 may be employed from time to ltime to assist inmaintaining the ports free from pluggingy A proportion of the recirculating. emulsion is continuously ,withdrawn by line 21 to settle1; 28 where the products stratify into a lower afid layer and an upper hydrocarbon layer. The acid is withdrawn by line 29, and all or any portion thereof may be recycled by pump 30 through line 3l to the acid. feed line- 20.. A small proportion of the acid may be continuously or intermittently discharged by line 33, While fresh make-up acid is added by line to maintain the catalyst at desired titratable acidity within the reactor. Preferably, a portion or all of the isobutane feed from line 2| may be passed through branch line 32` and emulsied With the recycle acid in line 3l and fresh make-up acid in. linev Z0 before the. latter is introduced into the reactor.

Hydrocarbon is continuously removed from the upper layer in settler 28 by line 34 and mixed with caustic soda solution introduced by linev 35, the mixture passing by line36 into conventional" neutralizing and settling equipment indicated generally at 3l. Settled caustic soda solution is Withdrawn by line 38', and al1y or any portion thereof recycled by pumpy 39 through line 410. A portion of the caustic sod-a solution may be continuously or intermittently discharged by line 4|, While fresh make-up NaOI-I solution is added by line 42.

The neutralized hydrocarbon is then passed by line t4 and pump 45 to a suitable stabilizing and fractonating system indicated by the fractionating tower 46. Excessisobutane is removed overhead by line 4l to condenser 48, and` thence by rundown line 49 to accumulator 50, from which uncondensed gas may' be released by line 54:.

Isobutane condensate is withdrawn by line. 52

and forced by pump 53 through recycle line 5t and branch lines 55 and 5t tothe isobutane feed lines 32 and 22 respectively. Stabilized alliylateV is Withdrawn by line 51 and fractionated in conventional manner tot recover a desired aviation fraction, or desired aviation and motor fuel fractions, from any heavier bottoms; It will be understood4 that Where a reneryl fraction, sucht as a C4. fraction, isv employed as the charge, the ofllgases removed by line. 41 in, the stabilization of the alhylate. Will contain some normal butano and: probably som-e propane in addition to isobutane: and; these offgases will be fractionated in conventional'. manner to recover a desired isobutane condensate for recycling through line 54.

Due to thev ine'- subdivision of the olen streams introduced through the openings or ports 2:5, and: due tothe' wide spacing of theseopenings throng-houtI a. substantial portion of the reaction zone, each olefin stream or seriesv of droplets is. eftectively mixed with a. relatively large volumeof the recirculating. emulsion. Conscquently,y even though the recirculating stream may be. travelingI at high. velocities,l the nely-divi'dedi olefin particle has substantially reacted by the time that particular increment of the recrculatlng stream moves past the next olefin introduction point. The disappearance of the olefin as such when finely divided in this manner in the positively-directed recirculating stream. occurs almost instantaneously, or within a few seconds.; at most. While, asy pointed out above, the allfiylation reaction ofy the isobuta-ne with the olefin is not. necessari-ly completed,y nevertheless the oleiinhas been converted to a forni in which it vrio-longer tends to. preferentially react with the acid or other .olen particles or molecules. Rather, the nely-divided olefin particle or droplet,` effectively surrounded. by arelatively large mass of. isobutanerin the presence ot the acid catalyst, and. wherein additional olefinparticlcs are; not brought into. contact and as. glomerated therewith,4 appears.- to; be, preieren-f, tially isolated soi that desiredV reaction with the isobuta-rieV is assured', Due to these effective re-y action` conditions', the necessity for extremely high velocities of ii'ow of. the recirculatingemul- J sion isavoided and powerr consumptionY maybe substantially reduced. The capacity of. the: plant; may be maintained or evenincreased with greatlyvlowered recirculation rates due tov the fact thatv theiconta'ct time for the. reaction. may be lowered to about 10 minutes. or event less.v It is to be understood that the reactor may be equipped: with suitable cooling or refrigerating coils for' controlling the temperature, as. is described in greater detail hereinbel'ow..

Fig. 2 discloses amodified form of reactor of the propellenm-ixer type having a shell 601, internal tube-l S'li, pump 62, acidi feed line S53', olefin and isobutane feed liney lltl and product offtakev lineV G5'. In this form, ahollowA porousl or perforated tube orcylinder 66 is mounted within the tube- G-lfthe said cylinder extending from a pointv adjacent pump 62 to the upper end' of tube Si@ Thiscylinderis provided with a plurality of olefin feed ports or openings 6T extending in this case throughout from r to l/ of the. length of the recirculating flow passage. Thev olen feed line 64 introduces the liquefied hydrocarbon into thev interior of cylinder 66, from which the olefin.v feed' is injected in a multitude of fine streams. of droplets. .at spaced points into the emulsion passing upwardly through tube: lil. This is indicated in thek drawing by small dots on the exposed face of cylinder lilik to. indicate the olefin feed ports or openings 6l which face the observer in this` Fig. 2, and by the.v short. flow lines around the sides and ends1 ot cylinder 66 toindicate olefin flow from similar ports,` at thev side of the cylinder which: are not exposed toview. The lower end` of. tube 66 facing; the recirculating stream is tapered into astream-'line extremity as indicated at68, to cut down' the resistance to ow. It will be understood that additional cylinders or a series of cylinders in the form of an annular ring may be mounted within the annular channel between tube Gl and casing 60, to be used in conjunction with or in place oi the interior cylinder 8B. The annular ring of cylinders might be conveniently connected to a suitable header or headers through which the olen feed is supplied by line 64. It is to be understood that various shapes and configurations of tubes or olen feed chambers can be employed, so long as the olen is introduced in iinely-divided form at a large number of points-spaced throughout a substantial extent of the `recirculating flow passage.

Fig. 3 discloses a further `modification of a reactor of the propeller-mixer type having an outer casing 89, an inner hollow tube 90, a pump 9|, and an oitake 92 leading to a suitable settler. Positioned within `the annular channel between casing 89 and tube 90 are a plurality of spaced annular rings 94 which are hollow and serve as supply chambers for-alkylating agent. Also positioned within the hollow tube 9B are a plurality of hollow members or chambers 95, also serving as `alkylating agent receiving and introducing means. Each of the members 94 and 95 is provided with a porous or perforate wall or walls forming ports or openings 9G for the introduction of the alkylating agent into the recirculating emulsion stream, as indicated in Fig. 3 by the dots and flow lines similar to the illustration for cylinder 65 of Fig. 2. Acid from line 86 emulsiied with isobutane from line 8l is introducedby line 38 into the reactor. The charge of olen, or mixture of isoparain and olen, from line 85 is supplied to the respective members 84 and 95 through branch lines 91, 98, 99 and |00.

While two annular rings 94 and two hollow disclike members 95 are shown, it will be understood Y that the number and shape thereofmay be varied. Preferably, these supply members are spaced at roughly equal distances throughout the length of the recirculating flow passage, whereby the alkylating agent is introduced in finely-divided form at a large number of spaced points extending throughout a substantial .portion of the reaction zone. Each individual member is provided with only a suiiicient number of `openings of small size such that the individual streams of droplets issuing from these openings are surrounded by aA relatively large mass of emulsion stream, whereby agglomeration of alkylating agent from different openings of the same member is avoided and local accumulation of alkylating agent is prevented.` The spacing of the respective elements 94 and 95 is such that alkylati'ng agent introduced from one element has substantially reacted ,by the time the recirculating emulsion stream passes from that element to thefnext in series. If desired, the elements S5 may be in the form of rings rather than discs or flat cylinders. Moreover, the openings in each of the members may be solely on the side facing toward or away from the direction of flow of the emulsion stream,v or may be solely on the edges so as to'be more effectively swept by the emulsion moving at right angles past these openings, or anycombination of the above may be employed. f f

The mixed olefin or isobutane-oleiin iced may be prechilled; and the prechilled supply of the liquid hydrocarbon in the annular chamber l2 of Fig. 1, the perforated-cylinder 6B of Fig. 2 or the perforated rings 94 and chambers 95 of Fig. 3,

effects a heat exchange with the emulsion passing in contact therewith in the coni-ined recirculating flow'path, thereby effecting a positive temperature control immediately in the reaction zone..

While the invention has been described above in connection with the recycle of emulsion, it is tov be understood that the invention is also applicable to an alkylation system employing hydrocarbon recycle. -In this case, the hydrocarbon recycle is introduced into an alkylation reaction zone containing the'alkylation catalyst of considerable extent or length, and the oleiinis intro-v duced in nely-divided form through la large:

number of spaced small openings extending throughout a substantial portion of the said reaction zone. Moreover, it is pointed out that the feature of effecting indirect heat exchange directly in the alkylation reaction zone and immediately adjacent or opposite the point of olen introduction, can be accomplished in another manner in the propeller-mixer type of reactors of Figs. l-3. For example,.the bundles of chilling tubes toi-which-refrigerating medium is supplied may be mounted within the reactor immediately adjacent or-along the spaced points of olefin introduction. I

lWhile the invention has been described as applied specincally to the propeller type of reactor, it is A:to beunderstood that the invention is applicable to any type of alkylation reactor having mechanically-maintained agitation, and wherein the alkylating agent is distributed in small droplets;,throughout a substantial portion of the agitatd mixture. For example, the invention can be vpracticed with a so-called Votator mixer, a rotary mixer, a turbo type reactor, or any other type designed to give substantial uniformity throughout the agitated reaction mixture.

While the invention' has been described above as particularly applied to the alkylation of an isoparaiin with an alkylating agent, it is to be understood that the invention is applicable to the alkylation of any organic compound having a readily replaceable hydrogen atom with a suitable alkylating agent. For example, the method and apparatus described herein can be employed for the alkylation of a normal parain with an olefin or other alkylating agent, employing a catalyst effective lfor this normal paraiiin alkylation, such has IIF -'BF3, aluminum Achloride with hydrogen chloride, and the like. Likewise, the invention is applicable to the alkylation of aromatics and hydroxyaromatics, such as benzene, toluene, xylene, phenol, cresci, etc., with an alkylating agent -such as anolefin, an alcohol, an alkyl halide,

etc. By way of `specilic examples, there is mentioned the alkylation of benzene with ethylene to produce ethyl benzene, an intermediate in the manufacture ofv styrene, the alkylation of chlorinated kerosene with benzene to produce socalled keryl benzene for detergents and wetting agents; and the preparation of alkylated phenols.

13 A in the presence of suitab-le alkylation catalysts as described. i

While the invention has been illustrated and described above in connection with a single reactor system or unit, it is to be understood that the invention is applicable to a multi-stage system employing concurrent or countercurrent floW of hydrocarbons and catalyst through the system, as Well as such a multi-stage system employing split feed of olefin by the multitudinous point injection method in each of a plurality of stages of the system. In fact, the present invention affords advantages in such a multi-stage system having split feed of olefin not now attainablev on a practical commercial scale by conventional equipment, such as the propeller type mixer. For example, in the present multi-stage system having Stratco mixers for each stage and using split olein feed between the stages, the full theoretical advantages cannot now be practically realized because of structural and operating limitations. Thus, it is customary to employ a full-size mixer operating at about the upper practical limit of recirculating capacity to obtain the desired contact ratio and contact time in the first stage. Consequently, the second and succeeding stages have to handle and recirculate the alkylate produced in the previous stage or stages in addition to the isoparaffin and olefin undergoing reaction therein. This means that the succeeding stages have to operate at reduced capacity or lower olefin feed rate to maintain these optimum conditions of contact ratio and contact time, as otherwise the succeeding mixers would have to be of impractically large size and operate with objectionably high power consumption. By employing the principles of the present invention, enabling the internal recycle rate and the contact time to be cut down for a given size unit with at least equivalent or better results, a multi-stage system with individual reactors of practical size and greatly decreased power consumption can be operated with all stages under optimum conditions and at full capacity, thereby realizing the full theoretical advantages of split olefin feed between the separate stages as Well as the new advantages and results of the multitudinous point olen introduction in each stage as set forth above.

Obviously many modifications and variations of the invention, as hereinbefore set forth, may be made without departing from the spirit and scope thereof, and therefore only such limitations should be imposed as are indicated in the appended claims.

We claim:

1. A process for the synthesis of hydrocarbons which comprises passing a stream of alkylatable hydrocarbons through a reaction chamber having permeable walls, passing a stream of corrosive mobile alkylation catalyst through said reaction chamber in intimate contact With said hydrocarbons, introducing into said reaction chamber through said permeable Walls a non-corrosive hydrocarbon fluid comprising oleiins, maintaining alkylation conditions within said chamber to effect reaction of said alkylatable hydrocarbons with said olens, and introducing said olens at such rate so as to avoid undesirably high concentrations of olefins in the reaction mixture and so as to interpose a relatively catalyst-free barrier between. the catalyst-hydrocarbon mixture and the walls of the reaction chamber.

2. A process as defined in claim 1 in which said catalyst comprises aluminum chloride, said alkylatable hydrocarbon is isobutane, said olefin is e-thylene, and said iiuid comprising olefins serves to remove heat of reaction.

3. In ythe alkylation of a low boiling isoparafi'ln with an olefin in liquid phase in the presence of a liquid alkylation catalyst under alkylation conditions, wherein a substantial body of the reaction mix having an isoparafn concentration in the hydrocarbon phase in excess of 40% by volume is mechanically recirculated in a confined flow path within a reaction zone to provide an in- -ternal isoparamn recycle to hydrocarbon feed ratio in excess of 10:1, while the recirculating reaction mix is chilled to remove exothermic heat of reaction, and a small stream of the reaction mix is withdrawn from the recirculating mix as fresh hydrocarbon feed and catalysts are added thereto; the improvement which comprises continuously introducing hydrocarbon feed including all the olefin, unmixed with catalyst, into the recirculating reaction mix in a very large number, in excess of 50, of simultaneously added tiny liquid feed droplets, each of less than 1/4 inch in diameter and down to about capillary size, said feed droplets being spaced on initial introduction both lengthwise and laterally throughout a major portion of the confined ow path within the reaction zone, and with the droplets spaced sufficiently from each other to avoid local buildup of unreacted olefin concentration in the reaction mix at any point thereof so as to provide an effective isoparain-olen contact ratio at the immediate point of olefin entry substantially in excess of 1500z1.

ARTHUR R. GOLDSBY. CLAUDE W. WATSON.

REFERENCES CITED The following references are of record in the file of this patent:

UNITED STATES PATENTS Number Name Date 1,333,328 Martin Mar. 9, 1920 1,941,111 Schlecht Dec. 26, 1933 1,971,852 Goebels Aug. 28, 1934 2,002,394 Frey May 21, 1935 2,024,680 Curtis Dec. 17, 1935 2,131,191 Roetheli Sept. 27, 1938 2,222,012 Amos Nov. 19, 1940 2,238,802 Altshuler Apr. 15, 1941 2,246,703 Thiele June 24, 1941 2,308,786 Smith Jan. 19, 1943 2,311,144 Wickham Feb. 16, 1943 2,312,719 Kuhl Mar. 2, 1943 2,317,901 Frey Apr. 27, 1943 2,322,482 Stahly June 27, 1943 2,335,704 Smith Nov. 30, 1943 

